US3505111A - Process and device for the continuous concentration-crystallization of sugar syrups - Google Patents

Process and device for the continuous concentration-crystallization of sugar syrups Download PDF

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Publication number
US3505111A
US3505111A US430435A US3505111DA US3505111A US 3505111 A US3505111 A US 3505111A US 430435 A US430435 A US 430435A US 3505111D A US3505111D A US 3505111DA US 3505111 A US3505111 A US 3505111A
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column
massecuite
unit
syrup
crystallization
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US430435A
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Jan Michal Malek
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    • C—CHEMISTRY; METALLURGY
    • C13—SUGAR INDUSTRY
    • C13B—PRODUCTION OF SUCROSE; APPARATUS SPECIALLY ADAPTED THEREFOR
    • C13B30/00—Crystallisation; Crystallising apparatus; Separating crystals from mother liquors ; Evaporating or boiling sugar juice
    • C13B30/02—Crystallisation; Crystallising apparatus
    • C13B30/022—Continuous processes, apparatus therefor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D9/00—Crystallisation
    • B01D9/0018—Evaporation of components of the mixture to be separated
    • B01D9/0031—Evaporation of components of the mixture to be separated by heating
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D9/00—Crystallisation
    • B01D9/0036—Crystallisation on to a bed of product crystals; Seeding
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D9/00—Crystallisation
    • B01D9/005—Selection of auxiliary, e.g. for control of crystallisation nuclei, of crystal growth, of adherence to walls; Arrangements for introduction thereof
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
    • B01J8/38—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it
    • B01J8/384—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it being subject to a circulatory movement only
    • B01J8/388—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it being subject to a circulatory movement only externally, i.e. the particles leaving the vessel and subsequently re-entering it
    • C—CHEMISTRY; METALLURGY
    • C13—SUGAR INDUSTRY
    • C13B—PRODUCTION OF SUCROSE; APPARATUS SPECIALLY ADAPTED THEREFOR
    • C13B30/00—Crystallisation; Crystallising apparatus; Separating crystals from mother liquors ; Evaporating or boiling sugar juice
    • C13B30/02—Crystallisation; Crystallising apparatus
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F13/00—Arrangements for modifying heat-transfer, e.g. increasing, decreasing
    • F28F13/06—Arrangements for modifying heat-transfer, e.g. increasing, decreasing by affecting the pattern of flow of the heat-exchange media
    • H—ELECTRICITY
    • H05—ELECTRIC TECHNIQUES NOT OTHERWISE PROVIDED FOR
    • H05H—PLASMA TECHNIQUE; PRODUCTION OF ACCELERATED ELECTRICALLY-CHARGED PARTICLES OR OF NEUTRONS; PRODUCTION OR ACCELERATION OF NEUTRAL MOLECULAR OR ATOMIC BEAMS
    • H05H1/00—Generating plasma; Handling plasma
    • H05H1/24—Generating plasma
    • H05H1/26—Plasma torches
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S159/00—Concentrating evaporators
    • Y10S159/03—Fluidized bed

Definitions

  • each recirculation circuit has two liquid columns connected to their heads and bottoms, the massecuite in one of said liquid columns having an upward movement caused by the thermic currents resulting from heating and from gaseous phase bubbles rising in said column, while the massecuite in the associated recycling column has a downward movement, interconnecting two successive circuits, and discharging at the end of said successive crystallizing steps the product composed of nearly uniform crystalline grains in suspension in the resulting molasses.
  • Another disadvantage of conventional equipment is the ice low heat transfer through the heating walls which are generally composed of short vertical tubes heated by steam.
  • This small heat exchange is due, on the one hand, to the slow massecuite circulation about the end of the boiling operation and, on the other hand, to the fouling which is produced consequently to the syrup and massecuite evaporation and partial decomposition on the heating surfaces, this decomposition being also a result of action of reducing sugars and amino acids present in the sugar syrups, and a source of coloration which lowers the quality of the product.
  • the main object of the present invention is to provide for avoiding these inconveniences by establishing a plant wherein the sugar syrup boiling process can be carried out under continuous working conditions, wherein the syrup or the massecuite will be subjected to an intense and relatively uniform mixing, and wherein the fouling of the heating surfaces will be avoided.
  • the sugar syrup to be concentrated and crystallised is supplied in continuous manner and subjected to a series of continuous successive unit heatings and to corresponding evaporations.
  • a gaseous phase such as air, relatively compressed and preferably saturated with steam, is introduced into the syrup or massecuite.
  • the rising gaseous bubbles including the steam are preferably subjected to a forced dispersion (i.e.
  • a device to be used to perform this process consists of a series of evaporating-concentrating-crystallizing vessels, called units, each one of said units comprising a first substantially vertical column heated in its lower part, where the hydrostatic-pressure exerted by the column content is sufiiciently high to avoid the ebullition of the syrup in this heated part, said column ending at its head in a liquid-vapor separation chamber connected with the base of the first column through a second column serving as a downcomer for recirculation of the boiling mass from said chamber.
  • the first column contains, in its upper part an expansion chamber for the syrup or massecuite arriving hot from the heated part of the column and at the head of this expansion chamber, a device for the forced dispersion of the steam and gaseous phase bubbles which are introduced and distributed into the syrup or the massecuite under the level of this device.
  • Said dispersing device is formed by a plurality of vertical partitions, allowing a free passage for the boiling mass between them massecuite in the column, while the introducing and distributing means consists generally of a bubbler.
  • the first evaporating crystallising unit comprises an inlet for the continuous supply of syrup to be treated and might be provided with a proportioning device of crystalline germs known as crystallization seed.
  • the last unit comprises a continuous outlet of the massecuite forming the product of the operation and each of said units comprises an inlet for massecuite coming from a previous unit, an outlet of the more concentrated massecuite for feeding a following unit, and an inlet for the syrup at a relatively lowrate to compensate for the consumption of said syrup due to evaporation and crystallization.
  • the lack of syrup ebullition in the heated part of the first column prevents any change of the concentration of said syrup in the heated area, and, in consequence, substantially suppresses the danger of fouling the heating surfaces, while reducing the thermic decomposition rate.
  • the process is conformity with this invention will use as the gaseous phase to be introduced into the content of the unit which is part of the boiling device, steam containing air and relatively compressed, in order to gen erate, in the unit, a fluidized bed formed by the sugar crystals, air, steam and molasses, the apparent average viscosity of this fluidized bed being much lower than the viscosity of the highly viscous massecuite in a conventional process, this decrease in viscosity resulting in improved circulation of the boiling mass.
  • FIGURE 1 is a diagrammatic section of a continuous boiling device for sugar syrups, composed of n evaporating-crystallizing units.
  • FIGURE 2 is an example of possible realisation of 4 a unit making part of a device similar to that of FIG- URE 1.
  • FIGURE 3 is a diagrammatic sectional view of a plant conforming to the invention and formed of four units.
  • FIGURES 4, and 6 are diagrammatic cross-sections of three embodiments of a device for vapor and gaseous phase bubble dispersion formed by a plurality of vertical partitions located in the first column of the unit conforming to the invention.
  • each concentrating-crystallizing unit forming part of a boiling device according to the invention and including it units is composed of a first cylindrical column 1a, 1b 1n containing, in its lower part, a heating enclosure formed by a shell 2a, 2b 2n with a bundle of vertical tubes 3a, 3b 3n fixed in plates 4a, 4b 4n and, in its upper part, a plurality of vertical partitions 5a, 5b 5n of a kneed chamber 6a, 6b 6n made in one or several sections, and of a second cylindrical recycling column 7a, 7b 7n connecting said chamber through a recycling kneed element 8a, 8b 8n with the base of the first column.
  • An inlet 9a is used to feed the first unit with fresh syrup to be treated and inlets 9b 9n are used to introduce into each unit the boiled mass coming from the previous unit in the series.
  • An inlet 10b in each unit intermediate the first and the last one of the series allows to feed this intermediate unit with fresh syrup to compensate for the consumption of the treated syrup transformed into vapors and into crystallized product.
  • An outlet 11a, 11b Iln is intended for exhausting vapors to conduit 12, and an outlet 13a, 13b 1311 allows the discharge of each unit or the continuous removal of the boiling mass produced.
  • Inlets and outlets 14a, 14b 14a ensure the inlet of the heating steam and the removal of condensate obtained.
  • Tubular bubblers 15b 1512 located beneath the heating enclosures, except for the first unit, are used for the introduction of steam saturated air.
  • the unit illustrated in FIGURE 2 has a shape somewhat diiferent from that of the units of FIGURE 1.
  • Its heating enclosure comprises a shell 16 with tubes 17 fixed in plates 18, is provided with an inlet and an outlet 19 for the feeding and the discharge of the heating fluid and is inclined with respect to the vertical line.
  • the bubbler 20 for introducing relatively compressed damp air is located above said heating enclosure in the unit, and the first column of said apparatus is flared at its upper part 21 in which it contains a plurality of partition walls 22 to help the dispersion of the upstream gaseous phase bubbles.
  • Said upper part 21 of the first column ends at the top by a chamber 23 integral with said upper part, this chamber being useful for the separation of gaseous phase, syrup or massecuite and comprising an outlet 24 for the exhaust of separated gaseous phase.
  • a pipe 25 is used to feed the unit with massecuite coming from another unit (not shown in the drawing) and a pipe 26 is used as an outlet for the concentrated massecuite to move to a following unit in the series (not shown in the drawing).
  • Inlet 27 and outlet 28 allow the introduction of syrup for compensating respectively the consumption in evaporation plus crystallization and the discharge of the apparatus.
  • the installation illustrated in FIGURE 3 comprises four units.
  • Each of said units comprises a cylindrical column 29a to 29d containing at its axis a recycling tube 30a to 30d opened at its two ends.
  • the lower end of said tube is narrowed and located in the substantially conical bottom area of the column 29a to 29d.
  • This central tube crosses, in the upper part of the column, the heating enclosure 31a to 31d comprising a bundle of vertical tubes 32a to 32d fixed in plates 33a to 33d connected to conduits 34a to 34d and 35a to 35d for the respective supply and discharge of the heating fluid.
  • right beneath the upper aperture of recycling tube 30a to 30d is situated an assembly of a plurality of vertical partitions 36a to 36a of the type shown in FIG- URE 4.
  • a bubbler 37a to- 37d is arranged in the column below the heating enclosure and is connected to pipes 38a to 38d for the inlet of damp and relatively hot air under a pressure higher than the hydrostatic pressure exerted by the content of the column at the bubbler level.
  • Pipes 39a, 39b and 39c are used for the transfer of the massecuite of a unit to the following unit while a pipe 39d is utilized for the discharge of the contents of the last unit.
  • a pressure controller 42 enables to apply in the two first units of the device a constant running pressure higher than that existing in the two other unit vessels.
  • a proportioning device 43a connected to the first unit is used for the introduction of crystalline germs of determined size into said first unit so as to start the production of uniform crystals in the intstallation.
  • the level 44a to 44d of the syrup or of the massecuite in each unit of the series during the running of the installation must be situated above the level of the assembly of vertical walls 36a to 36:1 in order that the running efiiciency should be a good one.
  • the set of substantially vertical partitions as illustrated in FIGURE 4 comprises several walls forming cylindrical sections of different diameters. These sections are joined concentrically by means of flat irons 45 welded, on the one hand, to the upper edges of theses sections and, on the other hand, to the end of the recycling tube 301: to 30d of the unit vessel.
  • said assembly is formed of seven parallel fiat planes 5 fixed between each other by means of stayed and bolted tie-rods 46, this set can be suspended in the upper part of the first column of the unit by means of lugs 47.
  • the assembly of substantially vertical partitions illustrated in FIGURE 6 comprises several undulated sheetplates 49 joined by means of tie-rods 48 bolted at their ends, so that the cross-section of this set has the shape of a honeycomb.
  • each recirculation circuit is continuously supplied with crude preconcentrated sugar solutions to compensate for syrup spent by evaporation and crystallization.
  • a device for the continuous concentrationcrystal lization of sugar syrups and massecuite comprising, in combination, a series of at least two vessel units, each one of which comprises a hollow column comprising means for introducing damp air into the column and having successively from the bottom to the top thereof a base-section, a heated enclosure connected to said base-section for generating a crystallizing mass, and an expansion chamber for the crystallizing mass arriving from said enclosure with which said expansion chamber communicates, and a set of substantially vertical partition walls for the forced dispersion of gaseous phase bubbles formed in the crystallizing mass below this set, a conduit ending in the basesection of said column, a gaseous/ liquid phases separating chamber interconnecting the top of said column and said conduit ending in the base-section of said column to recycle the crystallizing mass separated from the gaseous phase in the separating chamber, the said vessel units having an inlet for syrups to be treated, pipings interconnecting the conducts of two successive units to allow a free passage of the products from one unit to the
  • each vessel unit comprises an intake and an outlet for enclosure heating fluid, upper and lower perforated plates forming respectively the cover and bottom of said enclosure, and a bundle of tubes fixed endwise in the holes of said perforated plates for connecting the base section and the expansion chamber of the corresponding column through said heated enclosure.
  • a continuous concentration-crystallization device wherein the heated enclosure of each unit is located outside the corresponding column.
  • each conduit to recycle the crystallizing mass is located outside the column of the corresponding unit and wherein said conduit forms with said column an O- or D-shaped circuit extended in the vertical direction.
  • each conduit to recycle the crystallizing mass is located inside the column of the corresponding unit and wherein the lower orifice of this recycling conduit is located beneath the level of the heated enclosure through which said conduit passes.
  • a continuous concentration-crystallization device wherein the set of substantially vertical partition walls in the column of each unit, for the forced dispersion of the gaseous phase bubbles in the crystalizing mass, comprises flat walls arranged in parallel, stayed and bolted tie-rods interconnecting said walls, and means for fixing said set at the top of the column and at the bottom of the gaseous/liquid phases separating cham ber of said unit.
  • a continuous concentration-crystallization device wherein the set of substantially vertical partition walls in the column of each unit, for the forced dispersion of the gaseous phase bubbles in the crystallizing mass, comprises cylindrical walls having different diameters and arranged concentrically, and means for fixing said walls at the top of the column and at the bottom of the gaseous/liquid phases separating chamber of said unit.
  • a continuous concentration-crystallization device wherein the means for introducing damp air into the column is located in the base-section of the column.
  • a continuous concentration-crystallization device wherein the means for introducing damp air comprises a perforated tray located beneath the inlet for the crystallizing mass recycled into the associated base-section, and an air-inlet located under this perforated tray.
  • a continuous concentration-crystallization device wherein the means for introducing damp air into the column is located in the expansion chamber in the column.
  • a continuous concetitration-crystallization device wherein the means for introducing damp air comprises a perforated tube forming bubbles, a source of air mixed with steam, and a feeding tube passing through the column Wall and interconnecting said source and said perforated tube.

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  • Chemical & Material Sciences (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Biochemistry (AREA)
  • Plasma & Fusion (AREA)
  • Thermal Sciences (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Spectroscopy & Molecular Physics (AREA)
  • Jellies, Jams, And Syrups (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
  • Confectionery (AREA)
US430435A 1964-02-14 1965-02-04 Process and device for the continuous concentration-crystallization of sugar syrups Expired - Lifetime US3505111A (en)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
FR963824A FR1393567A (fr) 1964-02-14 1964-02-14 Procédé et dispositif de concentration-cristallisation en continu des solutions liquides telles que les sirops sucrés

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US3505111A true US3505111A (en) 1970-04-07

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US430435A Expired - Lifetime US3505111A (en) 1964-02-14 1965-02-04 Process and device for the continuous concentration-crystallization of sugar syrups

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US (1) US3505111A (enrdf_load_stackoverflow)
CH (1) CH440175A (enrdf_load_stackoverflow)
DE (1) DE1300880B (enrdf_load_stackoverflow)
ES (1) ES308623A1 (enrdf_load_stackoverflow)
FR (2) FR1393567A (enrdf_load_stackoverflow)
NL (1) NL6501748A (enrdf_load_stackoverflow)

Cited By (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3608611A (en) * 1968-09-21 1971-09-28 Teruo Oshima Method for recovering a rubberlike high molecular weight polymer
US3891395A (en) * 1970-12-17 1975-06-24 Escher Wyss Ltd Crystalliser with intergral pumping means
US4168211A (en) * 1975-08-18 1979-09-18 Pottharst Jr John E Distillation apparatus and method
DE3246791A1 (de) * 1981-12-22 1983-06-30 Pedro Alamo Madrid Moreno Verfahren zum umruehren von fluessigkeiten unter vakuum, insbesondere von viskosen zuckervorprodukten bzw. von dicksaft
US4398594A (en) * 1981-05-12 1983-08-16 Esmil Bv Apparatus for use in carrying out a physical and/or chemical process, for example a heat exchanger
US4403650A (en) * 1980-11-12 1983-09-13 Esmil Bv Apparatus for flow of a liquid medium
US4427053A (en) 1981-05-12 1984-01-24 Esmil Bv Apparatus and method for the concentration of a liquid by evaporation
US4747915A (en) * 1983-07-18 1988-05-31 Montedison S.P.A. Falling-film process for the cocurrent evaporation of a solution
US5230742A (en) * 1987-02-02 1993-07-27 A. E. Staley Manufacturing Co. Integrated process for producing crystalline fructose and high-fructose, liquid-phase sweetener
US5234503A (en) * 1987-02-02 1993-08-10 A.E. Saley Manufacturing Co. Integrated process for producing crystalline fructose and a high-fructose, liquid-phase sweetener
US5350456A (en) * 1987-02-02 1994-09-27 A. E. Staley Manufacturing Company Integrated process for producing crystalline fructose and a high fructose, liquid-phase sweetener
US5656094A (en) * 1987-02-02 1997-08-12 A.E. Staley Manufacturing Company Integrated process for producing crystalline fructose and a high-fructose, liquid phase sweetener
EP0788561A4 (en) * 1994-11-02 1999-11-10 Swenson Process Equip Inc CRYSTALIZING DEVICE AND METHOD
US20050183941A1 (en) * 2004-02-19 2005-08-25 Smith Strom W. High capacity angled tower
US9732068B1 (en) 2013-03-15 2017-08-15 GenSyn Technologies, Inc. System for crystalizing chemical compounds and methodologies for utilizing the same

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3859052A (en) * 1972-08-15 1975-01-07 Joh A Benckiser Chem Fab Gmbh Crystallization apparatus having pressure-liquid level control means
EP2308576B1 (de) * 2009-09-25 2015-11-04 Stefan Ebner Verdampfer

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US880629A (en) * 1907-06-14 1908-03-03 C Christianson Harry Method of crystallizing sugar.
US1860741A (en) * 1927-02-14 1932-05-31 Jeremiassen Finn Crystallization apparatus
US1945281A (en) * 1930-05-15 1934-01-30 Koppers Co Delaware Evaporating apparatus
US2042488A (en) * 1932-08-12 1936-06-02 Chem Ind Basel Process for evaporating liquids
US2426839A (en) * 1943-05-29 1947-09-02 Alexander B Morris Method and apparatus for cleaning or grading sand or the like
FR1104869A (fr) * 1954-05-14 1955-11-24 Fr De Const Mecaniques Soc Appareil à cuire, à fonctionnement continu, à allure variable et réglable pour la cristallisation des solutions sucrées
US3266556A (en) * 1962-02-14 1966-08-16 Malek Jan Michal Heat exchangers

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE77205C (de) * G. HEYDECKE, Meine, Hann Verfahren zur Beförderung des Auskrystallisirens des Zuckers aus den Füllmassen der Zuckerfabriken und Raffinerien, genannt Schaum-Krystallisation
DE115256C (enrdf_load_stackoverflow) *
DE90071C (enrdf_load_stackoverflow) * 1896-02-16 1897-01-06
FR524427A (fr) * 1915-01-04 1921-09-03 Leon Naudet Procédé et dispositif pour l'évaporation des jus sucrés
NL10124C (enrdf_load_stackoverflow) * 1918-12-24
DE1148524B (de) * 1957-04-01 1963-05-16 Gerhard Weidenfeld Stehender Verdampfer mit selbstregelndem Fluessigkeitsdurchlauf

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US880629A (en) * 1907-06-14 1908-03-03 C Christianson Harry Method of crystallizing sugar.
US1860741A (en) * 1927-02-14 1932-05-31 Jeremiassen Finn Crystallization apparatus
US1945281A (en) * 1930-05-15 1934-01-30 Koppers Co Delaware Evaporating apparatus
US2042488A (en) * 1932-08-12 1936-06-02 Chem Ind Basel Process for evaporating liquids
US2426839A (en) * 1943-05-29 1947-09-02 Alexander B Morris Method and apparatus for cleaning or grading sand or the like
FR1104869A (fr) * 1954-05-14 1955-11-24 Fr De Const Mecaniques Soc Appareil à cuire, à fonctionnement continu, à allure variable et réglable pour la cristallisation des solutions sucrées
US3266556A (en) * 1962-02-14 1966-08-16 Malek Jan Michal Heat exchangers

Cited By (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3608611A (en) * 1968-09-21 1971-09-28 Teruo Oshima Method for recovering a rubberlike high molecular weight polymer
US3891395A (en) * 1970-12-17 1975-06-24 Escher Wyss Ltd Crystalliser with intergral pumping means
US4168211A (en) * 1975-08-18 1979-09-18 Pottharst Jr John E Distillation apparatus and method
US4403650A (en) * 1980-11-12 1983-09-13 Esmil Bv Apparatus for flow of a liquid medium
US4398594A (en) * 1981-05-12 1983-08-16 Esmil Bv Apparatus for use in carrying out a physical and/or chemical process, for example a heat exchanger
US4427053A (en) 1981-05-12 1984-01-24 Esmil Bv Apparatus and method for the concentration of a liquid by evaporation
DE3246791A1 (de) * 1981-12-22 1983-06-30 Pedro Alamo Madrid Moreno Verfahren zum umruehren von fluessigkeiten unter vakuum, insbesondere von viskosen zuckervorprodukten bzw. von dicksaft
US4747915A (en) * 1983-07-18 1988-05-31 Montedison S.P.A. Falling-film process for the cocurrent evaporation of a solution
US5230742A (en) * 1987-02-02 1993-07-27 A. E. Staley Manufacturing Co. Integrated process for producing crystalline fructose and high-fructose, liquid-phase sweetener
US5234503A (en) * 1987-02-02 1993-08-10 A.E. Saley Manufacturing Co. Integrated process for producing crystalline fructose and a high-fructose, liquid-phase sweetener
US5350456A (en) * 1987-02-02 1994-09-27 A. E. Staley Manufacturing Company Integrated process for producing crystalline fructose and a high fructose, liquid-phase sweetener
US5656094A (en) * 1987-02-02 1997-08-12 A.E. Staley Manufacturing Company Integrated process for producing crystalline fructose and a high-fructose, liquid phase sweetener
EP0788561A4 (en) * 1994-11-02 1999-11-10 Swenson Process Equip Inc CRYSTALIZING DEVICE AND METHOD
US20050183941A1 (en) * 2004-02-19 2005-08-25 Smith Strom W. High capacity angled tower
US7731822B2 (en) * 2004-02-19 2010-06-08 Smith Strom W High capacity angled tower
US9732068B1 (en) 2013-03-15 2017-08-15 GenSyn Technologies, Inc. System for crystalizing chemical compounds and methodologies for utilizing the same

Also Published As

Publication number Publication date
CH440175A (fr) 1967-07-15
NL6501748A (enrdf_load_stackoverflow) 1965-08-16
ES308623A1 (es) 1965-06-16
FR1393567A (fr) 1965-03-26
FR86441E (fr) 1966-02-04
DE1300880B (de) 1969-08-07

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